Method for producing catalytically active wall flow filters

ABSTRACT

The present invention relates to a wall flow filter, to a method for the production and the use of the filter for reducing harmful exhaust gases of an internal combustion engine. Particle filters are commonly used for filtering exhaust gases from a combustion process. Also disclosed are novel filter substrates and their specific use in exhaust gas aftertreatment.

The present invention relates to a method for producing particlefilters. Particle filters are commonly used for filtering exhaust gasesfrom a combustion process. The invention also relates to novel filtersubstrates and their specific use in exhaust gas aftertreatment.

The exhaust gas of e.g. combustion engines in motor vehicles typicallycontains the harmful gases carbon monoxide (CO) and hydrocarbons (HC),nitrogen oxides (NO_(x)), and possibly sulfur oxides (SO_(x)), as wellas particulates that mostly consist of soot residues and possiblyadherent organic agglomerates. These are called primary emissions. CO,HC, and particles are the products of the incomplete combustion of thefuel inside the combustion chamber of the engine. Nitrogen oxides formin the cylinder from nitrogen and oxygen in the intake air when thecombustion temperatures locally exceed 1400° C. Sulfur oxides resultfrom the combustion of organic sulfur compounds, small amounts of whichare always present in non-synthetic fuels. For the removal of theseemissions, which are harmful to health and environment, from the exhaustgases of motor vehicles, a variety of catalytic technologies for thepurification of exhaust gases has been developed, the fundamentalprinciple of which is usually based upon guiding the exhaust gas thatneeds purification over a catalyst consisting of a flow-through or wallflow honeycomb structure (wall flow filter) and/or a catalyticallyactive coating applied thereupon and/or therein. The catalyst promotesthe chemical reaction of various exhaust gas components to form harmlessproducts, such as carbon dioxide and water, and at the same time removesthe fine soot particles in the case of a wall flow filter.

Particles may be very effectively removed from the exhaust gas with theaid of particle filters. Wall flow filters made of ceramic materialshave proved particularly successful. These have two end faces and areconstructed from a plurality of parallel channels of a certain length,which are formed by porous walls and which extend from one end face tothe other. The channels are alternately sealed in a gas-tight manner atone of the two ends of the filter so that first channels are formed thatare open at the first side of the filter and sealed at the second sideof the filter, and second channels are formed that are sealed at thefirst side of the filter and open at the second side of the filter. Inaccordance with the arrangement of the filter in the exhaust gas flow,one of the end surfaces here forms the inlet end surface and the secondend surface forms the outlet end surface for the exhaust gas. The flowchannels that are open at the inlet side form the inlet channels, andthe flow channels that are open at the outlet side form the outletchannels. The exhaust gas flowing into the first channels, for example,may leave the filter again only via the second channels and must flowthrough the walls between the first and second channels for thispurpose. For this purpose, the material from which the wall flow filtersare constructed exhibits an open-pored porosity. The particles areretained when the exhaust gas passes through the wall.

Wall flow filters may be catalytically active. The catalytic activity isachieved by coating the filter with a coating suspension which containsthe catalytically active material. Contacting the catalytically activematerials with the wall flow filter is referred to in the art as“coating”. The coating takes on the actual catalytic function andincludes storage materials and/or catalytically active metals that arefor the most part present by being deposited in a highly dispersed formon temperature-stable metal compounds, in particular metal oxides, witha large surface area. The coating for the most part takes place via theapplication of an aqueous suspension of the storage materials andcatalytically active components — also called a washcoat - onto or intothe wall of the wall flow filter. After the application of thesuspension, the substrate is generally dried and, if applicable,calcined at increased temperature. The coating may consist of one layeror be made up of multiple layers that are applied atop one another(multi-layered) and/or offset relative to one another (as zones) onto acorresponding filter. The catalytically active material can be appliedto the porous walls between the channels (so-called on-wall coating).However, this coating can lead to an unacceptable increase in the backpressure of the filter. With this as the background, JPH01-151706 andWO2005016497A1, for example, propose to coat a wall flow filter with acatalyst such that the latter penetrates through the porous walls (whatis known as in-wall coating). A zone is understood to mean the presenceof a catalytically active material (coating) on or in the wall of thefilter over less than the entire length of the wall flow filter.

So-called three-way catalysts are used for exhaust gas reduction forstoichiometrically burning engines. Three-way catalysts (TWCs) are wellknown to those skilled in the art and have been required by law sincethe 1980s. The actual catalyst mass here consists for the most part of ahigh-surface, oxidic substrate material, on which the catalyticallyactive components are deposited with the finest distribution. Theprecious metals of the platinum group, platinum, palladium and/orrhodium are particularly suitable as catalytically active components forcleaning stoichiometrically composed exhaust gases. For example,aluminum oxide, silicon dioxide, titanium oxide, zirconium oxide, ceriumoxide and mixed oxides thereof, and zeolites are suitable as substratematerials. What are known as active aluminum oxides having a specificsurface (BET surface, measured according to DIN 66132 -latest version onthe filing date) of more than 10 m²/g are preferably used. Moreover,three-way catalysts include oxygen-storing components to improve thedynamic conversion. These include cerium/zirconium mixed oxides whichare optionally provided with lanthanum oxide, praseodymium oxide and/oryttrium oxide. Meanwhile, zoned and multi-layer systems having three-wayactivity have also become known (US8557204; US8394348). If such athree-way catalytic converter is located on or in a particle filter,this is referred to as a cGPF (catalyzed gasoline particle filter; forexample EP 2650042B1).

The quality of a catalytically coated exhaust filter is measuredaccording to the criteria of filtration efficiency, catalyticperformance and pressure loss. In order to meet these differentrequirements, filters are provided, for example, with catalyticallyactive zones. As stated, the zones may be present on the walls of thecells or in the porous wall of the filter matrix.

There are two principal groups of manufacturing processes for producingthese catalytically active zones. Common to both method groups is thatthe coating suspension is introduced into the filter by applying apressure difference, that is to say by the presence of differentpressures at the two end faces of the filter. The coating suspensionmoves in the channels of the filter in the direction of the lowerpressure.

In this case, the first group additionally operates with an excess ofcoating suspension which is brought into the filter substrate by apressure difference and the excess coating suspension is removed fromthe channels again by a pressure difference reversal. In the presentcase, excess coating suspension means that the amount of suspension usedfor the coating process is significantly above the value which isrequired for the desired loading of the filter with catalytically activematerial. The excess of coating suspension can be removed from thefilter again by appropriate means, such as a pressure differencereversal. Within the scope of the invention, a pressure differencereversal is understood to mean that a pressure difference present at therespective ends of the wall flow filter is reversed, and consequentlyits sign changes. This pressure difference reversal therefore actscounter to the original coating direction.

The second group works without a pressure difference reversal and awashcoat excess, i.e. the entire amount of suspension provided andsupplied for the coating remains essentially in the substrate, i.e. >97% of the proportion of solids in the coating suspension.

Examples of the prior art are given below with respect to the two groupsof coating methods. The first group includes WO06021338A1, whichdescribes a method for coating a wall flow particle filter with acoating composition, wherein the wall flow filter is made of anopen-pored material, has a cylindrical shape with length L, and has aplurality of flow channels from an inlet end surface to an outlet endsurface, said channels being closed off in alternating fashion. Thecoating suspension is applied by perpendicularly aligning the flowchannels of the wall flow filter such that one end face is located atthe bottom and the second end face at the top, by introducing thecoating composition into the filter body through the flow channels ofthe wall flow filter that are open in the lower end face to a desiredheight above the lower end face by applying a pressure difference andremoving excess coating composition downward by applying a suctionpulse. The special modifications of the method in WO06042699A1 andWO11098450A1 are based on the same coating principle. A coatingapparatus using this method principle is presented in WO13070519A1.Here, too, an excess of coating suspension and the principle of applyingthe pressure difference reversal are used.

This coating principle is also suitable for producing particle filterswhich have zones with catalytically active material on the inlet andoutlet sides. In WO09103699A1, a method for coating filters with twodifferent washcoats is described, the method steps being that the filtersubstrate is oriented vertically, a first coating suspension is pumpedfrom below (pressure difference with highest pressure at the lower end),the excess coating suspension removed through suction (pressuredifference reversal) and the filter body is filled again from below withthe second washcoat after rotation by 180°, and the excess is removed bysuction. The filter is dried and calcined after the coating process. Thesame coating principle is disclosed in US7094728B2.

EP1716903B1 proposes a method for coating filter bodies in which, aftercoating, the filter is freed of too much of a coating dispersion byimmersion in a washcoat suspension by repeatedly applying pressurepulses to one end of the filter body in such a way that excess coatingsuspension is forced out of the filter body until it has reached itsoptimum coating weight. Here, too, the objective appears to be, interalia, the reduction of the exhaust back pressure of the filter. This isclearly in-wall coating.

The methods described in WO06021339A1, WO15145122A2 and WO0110573A2, forexample, belong to the second group of coating methods, in which thefilter bodies are coated without excess washcoat and without pressuredifference reversal. In this case, the perpendicularly oriented filtercarrier can be coated with the washcoat from the lower or the upper endface.

WO06021338A1, discloses a method for coating a wall flow particle filterwith a coating composition, wherein the particle filter is made of anopen-pored material, has a cylindrical shape with length L, and has aplurality of flow channels from an inlet end surface to an outlet endsurface, said channels being closed off in alternating fashion. Themethod is characterized in that the flow channels of the wall flowfilter are aligned vertically, so that one end face is located at thebottom and the second end face at the top, the filter is filled bydipping the lower end face of the wall flow filter into a defined,provided amount of the coating composition and by applying a negativepressure to the openings of the outlet channels in the upper end faceand sucking the entire quantity of the coating composition into theinlet and outlet channels through the openings of the inlet channels inthe lower end face. The amount of coating composition presented isselected according to the desired coating concentration and coatingheight. There is no pressure difference reversal after the applicationof the pressure difference for coating. The coating suspension ismeasured and not used in excess.

WO0110573A2 also describes a method for coating particle filters inwhich a measured amount of washcoat is applied from below to the filtercarrier. By applying a pressure difference (vacuum at the upwardlydirected end face), the charged amount of coating suspension is suckedinto the channels of the substrate. The substrate is then rotated andthe washcoat is distributed to the upper end of the substrate in thechannels by the action of an air jet of pressurized air. In this method,there is no reversal of the pressure difference, since the secondpressure pulse also points in the same direction as the first one withrespect to the movement of the washcoat and thus no pressure differencereversal takes place.

WO15145122A2 is another example of this group of coating methods. Incontrast to the methods described above, however, here a predefinedamount of coating suspension is applied as measured to the upper endface of the vertically oriented filter and is distributed in thechannels of the particle filter by applying a pressure difference(suctioning by applying a vacuum to the lower end face). No furtherpressure difference reversal takes place after this coating step.

However, there continues to be a need for wall flow filter substrateswhich are capable of providing optimal performance in the requirementtriangle of catalytic activity, filtration efficiency, and exhaust backpressure, particularly in the range of stoichiometrically burning sparkignition engines.

The object of the present invention is to specify a production processfor catalytically coated, ceramic wall flux filter substrates, which inparticular allows improved wall flux filter substrates to be generatedin comparison with the prior art. The wall flow filters produced in thismanner should be superior to the substrates correspondingly producedaccording to the prior art, especially with regard to the requirement ofas low an exhaust backpressure as possible with nevertheless sufficientcatalytic activity and filtration efficiency. It was also an object ofthe present invention to specify filter substrates produced by the aboveprocess and their use in the exhaust gas aftertreatment.

These and other aims evident from prior art are achieved by a methodhaving the features of claim 1 in question. The dependent claimsdependent on these claims relate to preferred embodiments of the methodaccording to the invention. Claims 7 - 10 are directed to the wall flowfilters themselves and their use.

By proceeding, in a method for the production of coated ceramic wallflow filters having at least two catalytically active zones, the wallflow filter having a first end face, a second end face and a length Land a porosity of at least 50% to at most 80% and a mean pore diameterof 5 - 50 µm, in such a way that the method comprises the followingsteps:

-   i) an excess of a first coating suspension is introduced into the    first end face by applying a pressure difference via the wall flow    filter;-   ii) with a pressure difference reversal, an excess of the first    coating suspension is removed from the wall flow filter;-   iii) a second coating suspension without excess is introduced into    the latter via the second end face by applying a pressure difference    via the wall flow filter,

The solution to the stated aim is attained extremely surprisingly, butin no less advantageous a manner. Surprisingly, it has been found thatby combining the two different methods described above to produce atleast two identical or different catalytically active zones on a carriersubstrate, new wall flow filters can be produced which represent anoptimum with regard to filtration efficiency, exhaust back pressure andcatalytic activity and can be adapted to the respective requirements ofthe exhaust system (FIG. 1 ).

The present invention is based on the combination of two coating methodsby means of which a wall flow filter known per se is impinged upon withcatalytically active materials and thus coated. Steps i) and ii) belongin some way to a first coating method and step iii) forms the secondcoating process. In this case, the sequence of the individual methodsteps is not critical in a first approximation. Thus, for example, stepiii) can also be carried out before step i). It is only important thatstep ii) always takes place after step i), but these steps do not haveto be carried out directly one after the other. Step iii) can also becarried out, for example, between steps i) and ii). It should also bementioned that other intermediate steps not mentioned here, such as, forexample, an intermediate drying or calcination or rotation of thesubstrate, can be carried out within the scope of the invention,provided that the inventive success thereof is not unduly impaired. Itshould also be mentioned that the coating can be carried out with ineach case identical or in each case different catalytically activematerials with and without intermediate drying.

In a preferred embodiment of the present invention, it is thereforeconceivable that into a vertically locked wall flow filter, a firstcoating suspension in excess is introduced into the wall flow filter viathe first end face by applying a pressure difference via the wall flowfilter, and an excess of the first coating suspension is then removedfrom the wall flow filter. Here, the pressure difference reversalremoves said excess coating suspension from the channels of the wallflow filter counter to the coating direction. A second coatingsuspension is introduced into the wall flow filter without excess viathe second end face by applying a pressure difference via the wall flowfilter. Drying takes place in each case after the introduction of thesecond coating suspension. However, it is also preferably possible forintermediate drying to take place before the introduction of the secondcoating suspension.

In a further preferred embodiment, a first coating suspension isintroduced into the vertically locked wall flow filter without excessfrom a first end face by applying a pressure difference between the endfaces of the wall flow filter. A second coating suspension is thenintroduced into the wall flow filter from a second end face with excessby applying a pressure difference between the end faces of the wall flowfilter. Only then, in a step which does not necessarily directly follow,is an excess of second coating suspension removed from the wall flowfilter by a pressure difference reversal counter to the coatingdirection. In turn, a drying step is carried out, wherein drying canoptionally also take place after the introduction of the first coatingsuspension and before the introduction of the second coating suspension.

As already indicated above, it is possible to remove the substrate fromthe vertical lock between the steps for introducing the respectivecoating suspension and to rotate it by 180° C. and again lock it.Alternatively, however, this rotation may also be omitted. Particularpreference is therefore given to a method as illustrated above in which,in step i), the first coating suspension is introduced into the wallflow filter from the lower, first end face and in step iii), the secondcoating suspension is introduced into the wall flow filter from theupper, second end face without releasing the wall flow filter from itslock in the interim. Again, step ii) can be carried out directly afterstep i) or only after step iii). In the latter case, the second coatingsuspension is simultaneously introduced into the wall flow filter withthe pressure difference reversal which occurs (step ii) to remove theexcess of coating suspension through step i). Consequently, this leadsto a substantially more compact method which can be implemented well androbustly in production.

In the method according to the invention, in a first step i) asuspension comprising catalytically active materials is introduced intothe filter, for example via the lower end face of the wall flow filter.For this purpose, the pressure difference which is used for the fillingis preferably between 0.05 bar and 4 bar, more preferably between 0.1and 3 bar and particularly preferably between 0.5 and 2.5 bar. Dependingon the viscosity of the suspension and the cell dimensions of the wallflow filter, this pressure difference is preferably selected such thatthe filling speed in the cells is between 10 mm/s and 250 mm/s,preferably between 20 mm/s and 200 mm/s and very preferably between 30mm/s and 180 mm/s. The filling of the channels of the wall flow filterwith the suspension produces, according to the invention, a coatingwhich constitutes less than the maximum length of the wall flow filter.In this case one speaks of one zone. The zone length may be > 15%, morepreferably 20% - 85%, most preferably 25% - 75%, and extremelypreferably 30% - 70% of the length L of the wall flow filter. In otheraspects of the invention, this coating may also extend only up to atleast 1.25 cm from the lower end face.

Excess coating suspension is preferably removed in step ii) by applyinga pressure pulse with a pressure difference reversal from the channelsof the wall flow filter downward, counter to the coating direction.According to the invention, the pressure pulse described in the pressuredifference reversal is in particular a measure which is sufficient tolargely free the larger ducts or pores (for example Q3 distribution ≥d50 of the pore diameter) through the wall from the catalytically activematerial present above or in said pores.

In the embodiments of the method according to the invention, it istherefore particularly advantageous that in the still moist state of thecoating suspension, which was introduced into the wall flow filter bystep i), a corresponding pressure pulse according to the invention isset counter to the coating direction (pressure difference reversal)which ensures that the large pores are blocked as little as possible bythe coating components of the catalytically active material. Intensiveinvestigations have shown that the volumetric flow of the exhaust gasflowing over the wall of a filter is accomplished in particular by largepores. If a pressure difference is applied to pores, the gas flowslaminarly through the pores. The volumetric flow is then proportional tod⁴. That is to say, 256 times as much gas flows through a 4 × largerpore diameter [d]. If these pores are freed of catalytically activematerial seated on or in the wall by at least one relatively shortpressure pulse, the exhaust gas flow can later flow through the wall ofthe ceramic filter without significantly higher exhaust back pressure.The catalytically active material can continue to be present on thesmaller pores, which make up the contribution of the overall porosity ofthe filter material, without excessively impeding the passing exhaustgas. The substrates produced in this way, in combination withcatalytically active coating zones, exhibit good catalytic activity withsufficient filtration efficiency and an exhaust backpressure which isreduced compared with the catalytically active filters of the prior art.

As a rule, the pressure pulse counter to the coating direction (pressuredifference reversal) only “blows free” or “sucks free” the largetraversing pores or channels which reach through the wall. However, thecatalytically active substance remains predominantly present on or inthe smaller pores of the filter walls. For further discriminationbetween large and smaller pores, it may preferably be beneficial for thepressure pulse to come to full deployment in a relatively short periodof time. The maximum pressure difference should be achieved within theorder of ≤ 0.5 s, more preferably at least ≤ 0.2 s and most preferably ≤0.1 s. The pressure pulse during the pressure difference reversal shouldnot exceed 400 mbar, more preferably 370 mbar and very preferably 350mbar, since otherwise too much of the excess coating suspension isremoved. A lower limit is commonly based on the fact that opening of thelarge pores takes place at all. The lower limit is therefore preferablyat least 100 mbar, more preferably at least 120 mbar and very preferablyat least 150 mbar. It should be noted that the conditions for thepressure pulse represent a pressure difference which is applied via thewall flow filter from a first end face to a second end face. The personskilled in the art knows how this can be achieved in terms of equipment.An optimal balance between exhaust back pressure, filtration efficiencyand catalytic activity of the wall flow filter is achieved by the largepores in particular being purged/cleared under suction.

It has been found to be advantageous if a pressureless holding time isincorporated before the pressure pulse is applied during the pressuredifference reversal. The holding time can be adapted depending on theproperties of the wall flow filter (porosity, wettability, waterabsorption capacity, etc.). The holding time is preferably between 0 sand 10 s, more preferably between 0 s and 5 s and particularlypreferably between 0 and 2 s.

The method according to the invention can be used both for theproduction of on-wall coatings and in-wall coatings. In the case ofon-wall coatings, as much of the catalytic coating as possible islocated on the wall and not in the pores of the wall. Accordingly, it ispreferred if the solid constituents of the suspension that can penetrateinto the wall of the filter are less than 20% by weight, more preferablyless than 15% by weight, and very preferably less than 10% by weightbased on the amount of solid constituents. In the case of in-wallcoatings, on the other hand, the suspension is in the pores of the wallof a wall flow filter to a large proportion of > 80% by weight, morepreferably > 90% by weight and very preferably > 95% by weight and more.Scanning electron microscope images are evaluated with the aid of astatistical gray scale evaluation in order to determine the proportionof washcoat in the wall of the wall flow filter and the proportion ofwashcoat on the wall of the wall flow filter. In this case, freepores/air appear black in a catalytically coated filter, while theheaviest elements appear to be white. By suitable selection of themeasurement settings known to the person skilled in the art, thedifference between active mass and filter substrate can be evaluated inthis way on the basis of the separation of the grayscale.

The different behavior of the respective coating suspension iscontrolled very decisively by the particle size distribution of thesolid particles in the suspension. On-wall coatings are preferablyachieved in that the catalytically active material contains high-surfacemetal compounds, in particular oxides, whose average particle diameter(DIN 66160 - latest version on the filing date) d50 of the Q3distribution in relation to the average pore diameter of the filter d50of the Q3 distribution is preferably > 1 : 6 and > 1 : 1 andparticularly preferably > 1 : 3 and > 1 : 2(https://de.wikipedia.org/wiki/Partikelgr%C3%B6%C3%9Fenverteilung). Anupper limit commonly forms the value to be estimated by the personskilled in the art as reasonable for corresponding on-wall coatings. Byproper selection of the mean particle separation, it is possible tocontrol how much of the catalytically active materials should bepositioned in the wall or on the wall of the wall flow filter. Thesmaller the particle diameters of the metal oxide components that areadvantageously stable at high temperatures, the larger the amount ofthese components that can be positioned in the small pores of the wall.For an in-wall coating, the particle diameter d99 of the Q3 distributionin the suspension should preferably be < 0.6 : 1, more preferably < 0.5: 1 and particularly preferably < 0.4 : 1 in relation to the averagepore diameter of the pores in the filter walls (d50 of the Q3distribution). This then makes it possible to produce wall flow filterswhich are shown, for example, in FIG. 5 .

In an advantageous embodiment of the present invention, the catalyticcoating of the wall flow filter produced in steps i) and ii) has apositive gradient for the amount of catalytically active material in thecoating direction. This means that fewer catalytically active materialsare present in the vicinity of the end face via which the coatingsuspension has been introduced into the wall flow filter after step ii)than is observed further towards the middle of the wall flow filter inthe longitudinal direction (FIGS. 3, 10 a ). It is particularlyadvantageous that an application zone thus produced according to theinvention has an amount distribution of catalytic material, measured inthe material/length unit so that, after removal of the plugs over arange of e.g. 15 to 40 mm from the coating inlet end, from 20% by weightto 70% by weight less is contained than in a subsequent coated region ofthe zone. Preferably, the amount of active components has a positiveconcentration gradient in the range of 20% to 100%, more preferably 25%to 90% in the coating direction on an e.g. 80 mm length of thesubstrate. The concentration gradient due to the different amount anddistribution of the catalytically active materials can be determinedgravimetrically, for example, by evaluating X-ray absorption data (XRFmeasurement) or by measuring the BET surface area of certain filtersections along the longitudinal axis of the filter.

In a further preferred embodiment of the present invention, a method aspreviously described (steps i) and ii)) is carried out. In addition,without rotating the wall flow filter in its orientation, during saidmethod or subsequently — with or without intermediate drying — a certainamount of a suspension comprising a catalytically active material(identical or different from the first) is applied to the upper end faceand is introduced into the vertically locked wall flow filter byapplying a pressure increase at the upper end face and/or pressurereduction at the lower end face (pressure difference) of the wall flowfilter, so that this coating extends to less than 100% of the length ofthe wall flow filter (step iii)). The length of this zone coating in thechannels adjacent to the first coating can be determined by the personskilled in the art. It is at least 20% and not more than 95% of thelength L of the wall flow filter. Preferably from 40% to 85%,particularly preferably from 50% to 70%. A possible embodiment isdepicted in FIG. 4 .

Another possibility of carrying out this method principle describedabove would be, for example, to orient the filter vertically, in step i)to fill it from below with a pressure difference with excess washcoat toa certain coating length, to remove excess washcoat via pressuredifference reversal (step ii), to rotate the filter by 180° and then toimmerse the lower end face in a predefined quantity of coatingsuspension and fill it with a pressure difference while applying avacuum to the upper end face with the suspension in the second channels(step iii).

With the method combination described above, particle filters withcatalytically active zones can be produced in the inlet and outletchannels as in the examples shown in FIGS. 2 and 3 . The two zones (10a, 10 b) do not have to overlap. Consequently, a range of at most 20%,preferably at most 10% and very preferably at most 5% of the length L ofthe wall flow filter can remain free - if desired. However, the coatingspreferably overlap at least 5%, more preferably up to 20% and verypreferably 7% - 15% of the length L of the wall flow filter. Thefiltration efficiency of the filter as a whole and in particular of thefree region can then be specifically adapted after drying to therequirements of the wall flow filter by a subsequent powder coating. Thepowder coating for increasing the filtration efficiency is known to theperson skilled in the art from the filtering technique under the termprecoat (e.g. US44010013).

As already indicated, in a further advantageous embodiment of thepresent invention, the process steps i) - iii) according to theinvention can be connected in such a way that with the verticallyoriented wall flow filter substrate, the introduction of the suspensionfrom the upper end face and the treatment of the coating after step i)with the at least one pressure pulse occur simultaneously. Here, bymeans of the at least one pressure pulse used to treat the coatingsupplied from below, the suspension applied to the upper end face of thewall flow filter at the top is also sucked or pressed into the wall flowfilter at the same time. This is therefore done stepwise in such a waythat first the suspension is introduced from below into the wall flowfilter, then the suspension is applied to the upper end face, and thenboth suspensions are treated with the at least one pressure pulse. Thisleads to a particularly preferred method, but in this way two identicalor different coatings can be introduced into the wall flow filter fromdifferent ends of the wall flow filter with just a small number ofsteps. As a result, filter architectures of FIG. 4 can be obtained, forexample.

As already stated, in general terms, the suspensions applied from thebottom or the top may be the same or different. It is optionallypossible to dimension both the first applied coating and the secondapplied coating as an on-wall coating or as an in-wall coating. In thisconnection, the following combinations of catalytically active coatingsin the wall flow filter are particularly preferred (E = inlet side, A =outlet side in the exhaust gas flow direction):

Type of coating E inlet A outlet On-wall/on-wall SCR coating ASC coatingOn-wall/on-wall TWC coating TWC coating On-wall/in-wall SCR coating ASCcoating On-wall/in-wall TWC coating TWC coating In-wall/on-wall SCRcoating ASC coating In-wall/on-wall TWC coating TWC coatingIn-wall/in-wall SCR coating ASC coating In-wall/in-wall TWC coating TWCcoating In-wall/in-wall SCR coating SCR coating

The present invention also relates to a catalytically coated ceramicwall flow filter produced according to the invention for the treatmentof exhaust gases of a combustion process. Further advantageousembodiments for the method just described also apply to the wall flowfilter specified here, provided that these influence thespatial-physical configuration of the filter.

As described, a very preferred wall flow filter has a catalyticallyactive coating in the channels, of which at least one coating is aporous on-wall coating with a gradient of the washcoat concentrationfrom the end face (for example FIGS. ⅘). In this form, the filter has nopreferred direction. However, it is preferably installed in the exhaustgas system of a stoichiometrically operated internal combustion enginesuch that the coating produced by coating with excess suspension andpressure difference reversal (steps i) and ii)) is located in the outletchannel when viewed in the flow direction (FIG. 1 ).

With the catalytically active wall flow filter according to theinvention, the catalytically active coating of the filter can beselected from the group consisting of three-way catalyst, SCR catalyst,nitrogen oxide storage catalyst, oxidation catalyst, soot-ignitioncoating, hydrocarbon storage. The catalytically active coatings used canbe located in the pores and/or on the surfaces of the channel walls ofthe filter.

In a final aspect, the present invention also relates to the use of thefilter according to the invention in a method for oxidizing hydrocarbonsand/or carbon monoxide and/or in a method for reducing nitrogen oxideoriginating from a combustion process, preferably that of an automobileengine. The filter according to the invention is particularly preferablyused in exhaust systems of an internal combustion engine as SDPF (SCRcatalyst coated on a wall flow filter) cGPF (3-way catalyst coated on awall flow filter), NDPF (NOx trap catalyst coated on a wall flow filter)or cDPF (diesel oxidation catalyst coated on a wall flow filter).

A further application is the removal of nitrogen oxides from leanexhaust gas mixtures by means of the SCR method. For this SCR treatmentof the preferably lean exhaust gas, ammonia or an ammonia precursorcompound is injected into the exhaust gas and both are conducted over anSCR-catalytically coated wall flow filter according to the invention.The temperature above the SCR filter should be between 150° C. and 500°C., preferably between 200° C. and 400° C. or between 180° C. and 380°C. so that reduction can take place as completely as possible. Atemperature range of 225° C. to 350° C. for the reduction isparticularly preferred. Furthermore, optimum nitrogen oxide conversionsare only achieved when there is a molar ratio of nitrogen monoxide tonitrogen dioxide (NO/NO₂ = 1) or the NO₂/NOx ratio = 0.5 (G. Tuenter etal., Ind. Eng. Chem. Prod. Res. Dev. 1986, 25, 633-636; EP1147801 B1;DE2832002A1; Kasaoka et al., Nippon Kagaku Kaishi (1978), 6, 874-881;Avila et al., Atmospheric Environment (1993), 27A, 443-447). Optimumconversions starting at 75% conversion are already achieved at 250° C.with simultaneous optimum selectivity with respect to nitrogen inaccordance with the stoichiometry of the reaction equation

only with a NO₂/NOx ratio of around 0.5. This applies not only to SCRcatalysts based on metal-exchanged zeolites but to all common, i.e.,commercially available, SCR catalysts (so-called fast SCRs). Acorresponding NO:NO₂ content may be achieved with oxidation catalystspositioned upstream of the SCR catalyst.

The injection devices used can be selected arbitrarily by the personskilled in the art. Suitable systems can be found in the literature (T.Mayer, Feststoff-SCR-System auf Basis von Ammoniumcarbamat [Solid SCRsystem based on ammonium carbamate], dissertation, Technical Universityof Kaiserslautern, 2005). The ammonia can be introduced into the exhaustgas stream via the injection device as such or in the form of a compoundwhich produces ammonia under ambient conditions. Suitable compounds are,inter alia, aqueous solutions of urea or ammonium formate, as well assolid ammonium carbamate. These can be taken from a provided sourceknown per se to the person skilled in the art and can be added to theexhaust gas stream in a suitable manner. The person skilled in the artparticularly preferably uses injection nozzles (EP0311758A1). By meansof these, the optimum ratio of NH₃/NOx is adjusted so that the nitrogenoxides can be converted into N₂ as completely as possible.

Wall flow filters having an SCR-catalytic function are referred to asSDPF. These catalysts frequently possess a function for storing ammoniaand a function whereby nitrogen oxides can react with ammonia to formharmless nitrogen. An NH₃-storing SCR catalyst can be designed inaccordance with types known to the person skilled in the art. In thepresent case, this is a wall flow filter which is coated with a materialthat is catalytically active for the SCR reaction and in which thecatalytically active material, commonly called the “washcoat,” ispresent in the pores of the wall flow filter. However, along with the -in the proper sense of the term - ‘catalytically active’ component, thiswall flow filter may also contain other materials, such as bindersconsisting of transition metal oxides, and large-surface carrier oxides,such as titanium oxide, aluminum oxide, in particular gamma-Al₂O₃,zirconium oxide, or cerium oxide. Also suitable as SCR catalysts arethose that are made up of one of the materials listed below. However, itis also possible to use zoned or multilayer arrangements or evenarrangements consisting of a plurality of components one behind theother (preferably two or three components) with the same materials asthe SCR component or different materials. Mixtures of differentmaterials on a substrate are also conceivable.

The actual catalytically active material used in this regard accordingto the invention is preferably selected from the group oftransition-metal-exchanged zeolites or zeolite-like materials(zeotypes). Such compounds are sufficiently familiar to the personskilled in the art. Preferred in this regard are materials from thegroup consisting of levynite, AEI, KFI, chabazite, SAPO-34, ALPO-34,zeolite β and ZSM-5. Zeolites or zeolite-like materials of the chabazitetype, in particular CHA or SAPO-34, as well as LEV or AEI areparticularly preferred. In order to ensure sufficient activity, thesematerials are preferably provided with transition metals from the groupconsisting of iron, copper, manganese, and silver. It should bementioned in this respect that copper is especially advantageous. Theratio of metal to framework aluminum or, in the case of SAPO-34, theratio of metal to framework silicon is normally between 0.3 and 0.6,preferably 0.4 to 0.5. The person skilled in the art knows how to equipthe zeolites or the zeolite-like materials with the transition metals(EP0324082A1, WO1309270711A1, WO2012175409A1, and the literature citedtherein) in order to be able to deliver good activity with respect tothe reduction of nitrogen oxides with ammonia. Furthermore, vanadiumcompounds, cerium oxides, cerium/zirconium mixed oxides, titanium oxide,and tungsten-containing compounds, and mixtures thereof can also be usedas catalytically active material.

Materials which in addition have proven themselves to be advantageousfor the application of storing NH₃ are known to the person skilled inthe art (US20060010857A1, WO2004076829A1). In particular, microporoussolid materials, such as so-called molecular sieves, are used as storagematerials. Such compounds, selected from the group consisting ofzeolites, such as mordenites (MOR), Y-zeolites (FAU), ZSM-5 (MFI),ferrierites (FER), chabazites (CHA), and other “small pore zeolites,”such as LEV, AEI, or KFI, and β-zeolites (BEA), as well as zeolite-likematerials, such as aluminum phosphate (AIPO) and silicon aluminumphosphate SAPO or mixtures thereof, can be used (EP0324082A1).Particularly preferably used are ZSM-5 (MFI), chabazites (CHA),ferrierites (FER), ALPO- or SAPO-34, and β-zeolites (BEA). Especiallypreferably used are CHA, BEA, and AIPO-34 or SAPO-34. Extremelypreferably used are materials of the LEV or CHA type, and here maximallypreferably CHA or LEV or AEI. Insofar as a zeolite or a zeolite-likecompound as just mentioned above is used as catalytically activematerial in the SCR catalyst, the addition of further NH₃-storingmaterials can, advantageously, naturally be dispensed with. Overall, thestorage capacity of the ammonia-storing components used can, in a freshstate at a measuring temperature of 200° C., be more than 0.9 g NH₃ perliter of catalyst volume, preferably between 0.9 g and 2.5 g NH₃ perliter of catalyst volume, and particularly preferably between 1.2 g and2.0 g NH₃/liter of catalyst volume, and very particularly preferablybetween 1.5 g and 1.8 g NH₃/liter of catalyst volume. Theammonia-storing capacity can be determined using synthesis gasequipment. To this end, the catalyst is first conditioned at 600° C.with NO-containing synthesis gas to fully remove ammonia residues in thedrilling core. After the gas has been cooled to 200° C., ammonia is thenmetered into the synthesis gas at a space velocity of, for example,30,000 h⁻¹ until the ammonia storage in the drilling core is completelyfilled, and the ammonia concentration measured downstream of thedrilling core corresponds to the starting concentration. Theammonia-storing capacity results from the difference between the amountof ammonia metered overall and the amount of ammonia measured on thedownstream side based on the catalyst volume. The synthesis gas is heretypically composed of 450 ppm NH₃, 5% oxygen, 5% water, and nitrogen.

Besides an SCR zone, the wall flow filter according to the invention mayalso include a downstream-positioned zone with an ammonia-oxidationcatalyst(s), also referred to as ammonia slip catalysts (“ASC”), tooxidize excess ammonia and prevent it from being released into theatmosphere. In some embodiments, the ASC may be mixed with an SCRcatalyst. In certain embodiments, the ammonia oxidation catalystmaterial may be selected such that it facilitates oxidation of ammoniainstead of NOx or N₂O formation. Preferred catalyst materials compriseplatinum, palladium, or a combination thereof. The ammonia oxidationcatalyst may include platinum and/or palladium supported on a metaloxide(s). In some embodiments, the catalyst is disposed on a largesurface area substrate including, but not limited to, alumina.

In some embodiments, the ammonia oxidation catalyst comprises a platinumgroup metal on a silicon-containing substrate. A silicon-containingmaterial may comprise a material such as: (1) silicon dioxide, (2) azeolite having a silica to alumina ratio of at least 200, and (3)amorphous silica-doped alumina having an SiO₂ content of ≥ 40%. In someembodiments, a platinum group metal is present on the substrate in anamount of about 0.1% by weight up to about 10% by weight of the totalweight of the platinum group metal and the substrate. Preferredmaterials for ASCs can be found, for example, in WO 2018183457A1, WO2018141887A1, WO 2018081247A1.

Very particular preference is given to the use of the wall flow filteraccording to the invention in a method for the simultaneous oxidation ofhydrocarbons and carbon monoxide and in a process for reducing nitrogenoxide. This process is preferably that which takes place in a three-waycatalyst in the stoichiometric exhaust gas. It is preferred if, inaddition to this wall flow filter, there is also a downstream orupstream three-way catalyst in the exhaust system. Optionally there arealso 2 separate three-way catalysts, particularly preferably oneupstream and one downstream of the wall flow filter according to theinvention in the exhaust gas system. The wall flow filter is veryparticularly preferably used as a cGPF with three-way function.

Wall flow filters with a catalytic activity that eliminates nitrogenoxides and hydrocarbons and carbon monoxide (HC, CO, and NOx) in thestoichiometric exhaust gas (λ = 1 conditions) are usually referred to ascatalyzed gasoline particle filters (cGPF). In addition, they canconvert the oxides of the nitrogen under rich exhaust gas conditions andCO and HC under lean conditions. For the most part, the coatingsconsidered here contain platinum group metals, such as Pt, Pd, and Rh,as catalytically active components, wherein Pd and Rh are particularlypreferred. The catalytically active metals are often deposited with highdispersion on large-surface oxides of aluminum, cerium, zirconium, andtitanium, or mixtures thereof, which may be stabilized by additionaltransition elements, such as lanthanum, yttrium, praseodymium, etc. Suchthree-way catalysts also contain oxygen-storing materials (for example,Ce/Zr mixed oxides; see below). For example, a suitable three-waycatalytic coating is described in EP1181970B1, EP1541220B1,WO2008113445A1, WO2008000449A2, to which reference is hereby made withregard to the use of catalytically active powders.

The requirements applicable to gasoline particle filters (cGPF) differsignificantly from the requirements applicable to diesel particlefilters (cDPF). Diesel engines without DPF can have up to ten timeshigher particle emissions, based on the particle mass, than gasolineengines without GPF (Maricq et al., SAE 1999-01-01530). In addition,there are significantly fewer primary particles in the case of gasolineengines, and the secondary particles (agglomerates) are significantlysmaller than in diesel engines. Emissions from gasoline engines rangefrom particle sizes of less than 200 nm (Hall et al., SAE 1999-01-3530)to 400 nm (Mathis et al., Atmospheric Environment 38 4347) with amaximum in the range of around 60 nm to 80 nm. Due to their low particlerelaxation time, small particles follow flowlines with almost noinertia. A random “trembling movement” is superimposed on this uniform,convection-driven movement. For this reason, the nanoparticles in thecase of GPF must mainly be filtered by diffusion separation. Forparticles smaller than 300 nm, separation by diffusion (Brownianmolecular motion) and electrostatic forces becomes more and moreimportant with decreasing size (Hinds, W.: Aerosol technology:Properties and behavior and measurement of airborne particles. Wiley,2nd edition 1999). For this reason, particular optimization with respectto filtration efficiency at low exhaust back pressure is particularlyimportant, especially in the case of a cGPF.

Various catalytic functions may also be combined with one another. Thethree-way catalysts just mentioned may, for example, be equipped with anitrogen oxide storage functionality (TWNSC). As stated above, thesecatalysts consist of materials that, under stoichiometric exhaust-gasconditions, impart to the catalyst the function of a three-way catalyst,and that have a function for the storage of nitrogen oxides under leanexhaust-gas conditions. These stored nitrogen oxides are regeneratedduring brief rich operating phases in order to restore storagecapability. The manufacturing of a corresponding TWNSC preferably takesplace by assembling materials that are used for the construction of athree-way catalyst and a nitrogen oxide storage catalyst. A particularlypreferred embodiment of such a catalyst is described in WO2010097146A1or WO2015143191 A1, for example. However, during the regeneration, anair/fuel mixture is preferably maintained which corresponds to a λ of0.8 to 1. This value lies particularly preferably between 0.85 and 0.99,and very particularly preferably between 0.95 and 0.99.

All ceramic materials customary in the prior art can be used as wallflow monoliths or wall flow filters. Porous wall flow filter substratesmade of cordierite, silicon carbide, or aluminum titanate are preferablyused. These wall flow filter substrates have inflow and outflowchannels, wherein the respective downstream ends of the inflow channelsand the upstream ends of the outflow channels are alternately closed offwith gas-tight “plugs.” In this case, the exhaust gas that is to bepurified and that flows through the filter substrate is forced to passthrough the porous wall between the inflow channel and outflow channel,which delivers an excellent particle filtering effect. The filters maybe symmetrical or asymmetrical. This means that the inflow channels areeither just as large as the outflow channels or else the inflow channelsare larger than the outflow channels, i.e., they have a larger so-called“open frontal area” (OFA) than the outflow channels. The filtrationproperty for particulates can be designed by means of porosity,pore/radii distribution, and thickness of the wall. The open porosity ofthe uncoated wall flow filters is typically more than 50% up to amaximum of 80%, generally from 50% to 75%, particularly from 50% to 70%[measured according to DIN 66133, latest version on the filing date].The average pore diameter d50 of the uncoated filters is at least 5 µm,for example from 7 µm to 35 µm, preferably more than 10 µm, inparticular more preferably from 10 µm to 25 µm or very preferably from15 µm to 20 µm [measured according to DIN 66134, latest version on thefiling date]. The completed filters having a mean pore diameter (d50) oftypically 10 µm to 25 µm and a porosity of 50% to 65% are particularlypreferred.

Each of the known production methods for applying the catalytic coatingdescribed above as prior art has advantages and disadvantages inso-called in-wall coatings or on-wall coatings in the filter, generallydepending on which zone is located on the input side or output side ofthe filter in the exhaust air flow. In principle, the zone in the wallof the filter, irrespective of the group of processes by which it isproduced, has poor filtration properties and poor performance but a verylow pressure loss. The method with reversal of the pressure differenceand with excess coating suspension during coating (group 1) has anaverage catalytic performance, an average filtration efficiency and anaverage pressure loss in application zones. The process without reversalof the pressure difference and without excess of coating suspensionduring coating (group 2) has good catalytic performance and filtrationefficiency in application zones, but has a very high pressure loss.

The wall flow filter according to the invention considered here hasobtained its decisive character by the type and manner of coating. Thestarting point is a catalytic coating applied in special form to thefilter, which is made porous by the application of a pressure pulsecounter to the coating direction (pressure difference reversal) andtherefore has a desired high permeability. This coating is combined witha coating which is embodied in the adjacent channels as an in-wall oron-wall coating, which has not been subjected to a pressure differencereversal. This filter produced by combining the two coating variants hassurprising advantages over coated wall flow filters which were producedonly according to one of the coating principles shown. In particular,optimized particle filters can be produced with such embodimentsaccording to the invention, which can be tailored precisely to therespective application purpose or the respective exhaust gas problem.Against the background of the known prior art, this was not to beexpected.

FIGURES

FIG. 1 shows by way of example the effect of different combinations ofthe different coating architectures on the basis of Pattern 1 (top) - 4(below). With regard to their effect in the exhaust gas flow. Thecombination of two coatings with high permeability has the lowestpressure loss, but is otherwise weaker in filtration efficiency,light-off temperature and OSC (oxygen storage) than the other patternsof the present invention. The combination of two coatings with lowpermeability shows very good values with regard to light-offtemperature, OSC and filtration efficiency, but results in an enormousincrease in pressure. The best combination of all features (pressureloss, filtration efficiency, light-off temperature and OSC) shows thecombination of a low permeability coating in the input cell (inlet sideof the filter in the exhaust gas; E) with a porous coating according tothe invention with a high permeability in the starting cell (outlet sideof the filter in the exhaust gas; A). The optimum setting of the twozone lengths depends on the requirements of the respective motor. Thequality criteria of the coated filter can thus be adjusted via the zonelength as with a slide controller.

FIG. 2 shows schematically the product with two application zonesresulting from the combination of the coating methods. On the porousbasic matrix of the filter 100 with the plug 160 is a porous coating400, also termed a filter cake, with a high permeability, produced bythe coating from below with an excess and a pressure differencereversal, and a low-porosity coating 500 with a low permeability,produced by the coating from above without pressure difference reversal.The exhaust gas 600 flows over the coating 500 and flows through theporous matrix of the filter 100 and the open-porous coating 400. Afterthe flow, the layer 400 is also overflowed.

FIG. 3 relates to the combination of an on-wall coating (10 a) producedaccording to the invention and an additional in-wall coating (10 b)coming from the other side. The preferred embodiment with an overlap isshown.

FIG. 4 The figures show four exemplary embodiments of Pattern 1 toPattern 4 from the experimental part

FIG. 5 shows the coating concentration along the longitudinal directionof two inventive (Pattern 2 and 3 respectively) and two non-inventivewall flow filters (Pattern 1 and 4). All three variants have in totalthe same amount of coating as loading. The five disks per variant wereshown (standardized) relative to the loading of the first disks on theleft. The distribution of the oxide loading over the length of thefilter measured via the determination of the BET surface is shown by wayof example for various combinations of coatings for two zones on thewall.

FIG. 6 shows the permeability distribution of two application zonesproduced according to the invention

EXAMPLES

The exemplary experiments for the preparation of filters withapplication zones were carried out with the following startingmaterials.

Filter substrates: Cordierite, 4.66” × 4.66” × 6.00”, 300/8, averagepore diameter d50 = 17.5 µm

Noble metal loading: 36 g/ft³ (Pt = 0 / Pd = 30 / Rh =6)

Oxide loading: 100 g/L

Specification for the particle-column distribution of the on-wallcoatings: d50=4.2 - 5.0 µm, d90 = 9.0 - 18 µm

Distribution of washcoat coating in the wall flow filter:

Since the filter used for pattern production has a volume of 1.68liters, the oxide loading is 168 g. If only a zone of 80% of the lengthis applied, the zone for these comparisons contains the 168 g. If twozones with 60% of the length L of the filter are applied, each zonecontains 50% of the oxides and thus 84 g of oxide. If a zone with 80% ofthe substrate length were combined with a zone with 40% of the substratelength, the 80% long zone in this comparison would have ⅔ of the amountof oxide (= 112 g) and the 40% long zone would have ⅔ of the amount ofoxide (= 56 g).

Experimental part for the production of the zoned outlay Pattern 1 - 4:

General

Aluminum oxide stabilized with lanthanum oxide was suspended in waterwith a first oxygen storage component, which comprised 40% by weightcerium oxide, zirconium oxide, lanthanum oxide and praseodymium oxide,and a second oxygen storage component, which comprised 24% by weightcerium oxide, zirconium oxide, lanthanum oxide and yttrium oxide. Bothoxygen storage components were used in equal parts. The suspension thusobtained was then mixed with a palladium nitrate solution and a rhodiumnitrate solution under constant stirring. The resulting coatingsuspension (washcoat) was used directly to coat a commercially availablewall flow filter substrate.

In the following, the methods for producing products are described whicheach have two application zones which have been coated by different endfaces of the filter and each extend over approximately 60% of the lengthof the filter. The loading of the finished catalysts is composed of 100g/L of ceramic oxides and 36 g/cft (= 1.27 g/L) of noble metal (ratio ofpalladium to rhodium 5: 1), which at the filter volume of 1.6761 Lcorresponds to a total oxide loading of 167.6 g/filter and a total noblemetal amount of 2.13 g/filter. The ratio of ceramic oxides to noblemetals is the same in the washcoat of both zones and constant over theentire filter. The total oxide and noble metal amount is equally dividedinto the two zones during the coating, as a result of which an oxideamount of 83.55 g and a noble metal amount of 1.07 g are ideally appliedin each zone coating step.

Pattern 1 (Non-Inventive)

Both washcoat zones a) and b) of Pattern 1 (FIG. 4 a) were producedusing the same coating method, the ceramic suspension first beingintroduced into the filter in excess by applying a pressure difference(pressing from below). The excess of oxides is removed by a pressuredifference reversal, i.e., the renewed application of a pressuredifference (suction from below) opposite the first.

First, zone a) is coated from the bottom from end face A. For thispurpose, the suspension has a solids content of around 33% and ispressed into the substrate until 60% of the substrate length is filledwith washcoat from bottom to top. The excess washcoat is removed fromthe filter with a short suction impulse counter to the coating direction(approx. 330 mbar negative pressure, 1.5 sec). After drying andcalcining, the filter is coated from the bottom from the front side B inorder to produce zone b). The coating is effected analogously to thecoating of zone a), only the coating parameters differ slightly (solidsconcentration of around 35%, suction pulse negative pressure around 210mbar, suction pulse duration around 0.5 sec., increase in the suctionpulse within 0.2 sec to the maximum). The filter is dried and calcined.

Pattern 2 and Pattern 3 (Inventive)

Pattern 2 (FIG. 4 b ) and Pattern 3 (FIG. 4 c ) were produced accordingto one procedure, the coating of zone a) and zone b) each having adifferent coating process.

First, zone a) is coated from the bottom from end face A. For thispurpose, the suspension has a solids content of around 34% and ispressed into the substrate until 60% of the substrate length is filledwith washcoat from bottom to top. The excess washcoat is removed fromthe filter with a short suction pulse (around 330 mbar negativepressure, 1.5 sec suction pulse duration, rise in the suction pulsewithin 0.2 sec to maximum). After drying and calcining, the filter iscoated from the top from the front side B in order to produce zone b).For this purpose, a measured washcoat quantity (solids content about44%) is added from above to the front side B and a short suction pulse(250 mbar negative pressure, 3 sec) is applied in order to distributethe washcoat in the filter. The filter is dried and calcined.

Sample 4 (Non-Inventive)

Both washcoat zones a) and b) of Pattern 4 (FIG. 4 d ) were producedusing the same coating method, the ceramic suspension being applied fromabove to the wall flow filter and brought into the filter by applying apressure difference (suction from below) (non-inventive).

First, zone a) is coated from the front face A from above. For thispurpose, the suspension has a solids content of 43 - 45% and is added ina metered amount from above to the front side A. A pressure differencein the form of a short suction pulse (250 mbar negative pressure, 1 sec)is applied in order to distribute the washcoat in the filter. Afterdrying and calcining, the filter is coated from the top from the frontside B in order to produce zone b). The coating parameters for this areanalogous to those for coating zone a). The filter is dried andcalcined.

Characterization

The effectiveness of a catalytically active filter is determined by theinteraction of the functional groups of catalytic performance,filtration efficiency and exhaust back pressure (backpressure) whichessentially result from the distribution of the catalytic material andthe permeability of the washcoat layers. The distribution and quantityof the catalytically active material in the flow direction of the filteris determined via a measurement of the BET surface (DIN 66132 - latestversion on filing date), and the permeability is determined by measuringthe back pressure on filter samples of Patterns 1 to 4.

Analysis of the gradient of washcoat distribution and permeability:

The samples for the analyses with respect to the determination of thegradients (determination of the distribution of the catalytic materialin the axial longitudinal direction) were prepared after coating andcalcination as follows:

-   Cutting off the filter plugs on both sides (filter shortened by 2×10    mm)-   Dividing the residue in the longitudinal direction to 5 equal-length    parts (filter disks)-   To determine the BET gradient, the 5 disks were ground and analyzed.

For the permeability measurement, a block of 10 mm x 10 mm x 20 mm(width x depth x height) was sawed out of each disk in the center. Eachsecond channel was clogged alternately to produce a small minifilter.For this minifilter, the pressure loss is measured at an air flow of 6I/min. The pressure loss is initially set to be proportional to thepermeability.

FIG. 5 shows by way of example the differences in washcoat loading(gradients in the disks) between the five filter sections with respectto the BET surface, which result from the use of the different methodsa) coating with excess washcoat and changing direction of the pressuredifference and b) coating without and only with a low level of washcoatexcess without an alternating pressure difference for the combination ofthe on-wall zones. The suspensions used had identical particle sizedistributions and identical Pd to oxide ratios. Due to the differentmethods, the suspensions had different viscosities and different solidsconcentrations. The gradient was always standardized with the value ofthe left disk.

All 3 variants (Pattern 1, Pattern 2/3, Pattern 4) have in total thesame amount of washcoat as loading. The 5 disks per variant was shown(standardized) relative to the loading of the first disks on the left.Thus, the left disk always has 100%.

In the coating according to the method according to the invention(coating with excess washcoat and changing direction of the pressuredifference according to method steps i) to iii)), an increasing gradientresults in the coating direction, while a uniform distribution of thecatalytic material without gradient results in the coating withoutpressure difference reversal. The effect of the coating methods on thepermeability is shown in FIG. 6 by way of example for Pattern 2.

FIG. 6 shows the course of the permeability by way of example for thecombination of two on-wall zones, wherein the left zone was producedwith a washcoat excess and a reversal of the pressure difference duringthe coating according to method steps i) to ii) of the first preferredembodiment of the method, while the right zone was produced withoutexcess washcoat and without reversal of the pressure difference. Bothzones contain the same amount of oxides and both cover 60% of the lengthof the filter.

To determine the permeability, the plugs of the filter were firstremoved. The remainder was divided into 5 equally long disksapproximately 26 mm in length. Small cuboids with a base area of 10 mm ×10 mm and a height of 26 mm were in turn produced from the disks. Thechannels were thus provided with plugs, so that 5 small filter bodieswere produced. A pressure difference volume flow curve was nowdetermined for the small filters and the permeability was calculated viathe Darcy equation. The left zone was used to standardize thepermeability of the five small filters.

The first disk of the zone, hereinafter referred to as region A, whichwas produced with excess washcoat and a reversal of the pressuredifference during coating, has a permeability of 4 to 20 times higher inthe first 15 to 50 mm than the zone in the following mm. The length Lwas measured from the end face after removal of the plugs, which had thefirst contact with the washcoat in the case of coating with excesswashcoat and a reversal of the pressure difference. The zone which wasproduced without excess washcoat and without reversal of the pressuredifference during coating has a permeability which corresponds to only5% to 25% of the permeability of region A with the same particle sizedistribution of the oxides in the washcoat and the same amount of oxidein the zone. The same applies to the region of the zone which has beenproduced with a washcoat excess and a reversal of the pressuredifference during the coating, which is further away from the end facethan the region A.

Table 1 shows the distribution of the oxides and the resultingpermeability in a zone produced from below after process steps i) toiii) (the length measurement starts after the plug). The range 0 - 26 mmwas used for standardization to 100%

TABLE 1 0 mm - 26 mm 26 mm - 52 mm Oxide loading 100% 132% Permeability100% 12%

In comparison, table 2 shows the different permeabilities of thecoatings from top and bottom (the length measurement starts behind theplug). The range 0 - 26 mm of the coating from below was set at 100% forstandardization.

TABLE 2 Permeability in the first 26 mm behind the plug Coating frombottom 100% Coating from the top 16%

Catalytic Characterization of the Products

In the foregoing, after Patterns 1 to 4 have been characterized withrespect to the distribution of the catalytic material and thepermeability, the catalytic efficiency, filtration efficiency, andexhaust back pressure of the four different patterns are subsequentlydetermined.

The particle filter Patterns 1 to 4 were co-subjected to engine testbench aging. This aging process consists of an overrun cut-off agingprocess with an exhaust gas temperature of 950° C. before the catalystinlet (maximum bed temperature of 1030° C.). The aging time was 19 hours(see Motortechnische Zeitschrift, 1994, 55, 214-218).

The catalytically active particle filters were then tested in the agedstate at an engine test bench in the so-called “light-off test”, in the“lambda sweep test” and in the “OSC test”. In the light-off test, thelight-off behavior is determined in the case of a stoichiometric exhaustgas composition with a constant average air ratio λ (λ=0.999 with ±3.4%amplitude).

Table 3 below contains the temperatures T70 of Patterns 1 to 4, at which70% of the considered components are respectively converted.

TABLE 3 # T70 HC stoichiometric T70 CO stoichiometric T70 NOxstoichiometric 1 403 431 431 2 401 424 429 3 396 413 417 4 392 406 409

The dynamic conversion behavior of the particle filters was determinedin a lambda sweep test in a range from λ = 0.99 - 1.01 at a constanttemperature of 510° C. The amplitude of λ in this case was ±3.4%. Table2 shows the conversion of Patterns 1 to 4 at the intersection of the COand NOx conversion curves, along with the associated HC conversion ofthe aged particle filters.

TABLE 4 # CO/NOx conversion at the intersection HC conversion at theCO/NOx intersection 1 95% 96% 2 95% 96% 3 96% 97% 4 96% 96%

The particle filter Pattern 2 shows a slight improvement in light-offbehavior compared to Pattern 1 in the aged state. The particle filtersof Patterns 3 and 4 show a marked improvement in light-off behavior anddynamic CO/NOx conversion in the aged state compared with Pattern 1.

In order to calculate the oxygen storage capacity of the particlefilters in mg/L, the particle filter was placed between two lambdaprobes and the time offset of the two sensor signals was measured duringa jump test (OSC test) with lambda jumps of λ = 0.96 - 1.04(Autoabgaskatalysatoren, Grundlagen -Herstellung - Entwicklung -Recycling - Ökologie, Christian Hagelüken, 2nd edition, 2005, p. 62).Table 5 shows the results of the OSC tests of Patterns 1 to 4.

TABLE 5 # OSC [mg/L] 1 159 2 166 3 199 4 196

Patterns 3 and 4 show a markedly increased oxygen storage capacity afteraging compared to Pattern 1.

The particle filters in Patterns 1 to 4 were compared at a cold blowtest bench with respect to the exhaust back pressure.

Table 6 below shows pressure loss data which were determined at an airtemperature of 21° C. and a volume flow rate of 300 m³/h.

TABLE 6 # bp @ 300 m3/h bp @ 300 m3/h (relative to #1) 1 28.8 mbar - 243.2 mbar + 50% 3 40.5 mbar + 41% 4 64.9 mbar + 125%

The combination of two layers, each produced by a coating methodaccording to steps i) - ii) (Pattern 1), has the lowest pressure loss.The combination of two layers, each produced by a coating process in theabsence of steps i) - ii) (Pattern 4), results in an enormous increasein pressure compared to Pattern 1. The two patterns in which the coatingprocesses for Zone a) and Zone b) differ have an acceptable increase inthe pressure loss with respect to Pattern 1, but have a significantlylower pressure loss compared to Pattern 4.

The particle filters described were investigated for their freshfiltration efficiency on the engine test bench in the real exhaust gasof an engine operating on average with stoichiometric air/fuel mixture.A globally standardized test procedure for determining exhaustemissions, or WLTP (worldwide harmonized light vehicles test procedure)for short, was used here. The driving cycle used was WLTC Class 3. Theparticle filters were installed 30 cm downstream of a conventionalthree-way catalyst which was the same for all particle filters measured.In order to be able to detect particulate emissions during testing, theparticle counters were installed upstream of the three-way catalyst anddownstream of the particle filter. Table 7 shows the results of thefiltration efficiency measurement.

TABLE 7 # FE [%] 1 77 2 86 3 82 4 91

Pattern 1 has the lowest filtration efficiency, in which both zones wereeach produced by the same coating method as in steps i) - ii). Incontrast, Pattern 4 in which both zones were also produced by the samecoating method, but which differed from that for Pattern 1 by excludingsteps i) - ii), has the highest filtration efficiency. Although the twoPatterns 2 and 3, in which the coating processes for zone a) and zone b)differ and were produced in accordance with steps i) to iii), have alower filtration efficiency than Pattern 4, they result in a significantincrease in filtration efficiency compared to Pattern 1.

FIG. 1 shows by way of example a summary of the effect of differentcombinations of different on-wall washcoat layers with a view to theeffect in the exhaust gas flow. The combination of two layers with ahigh permeability, each produced via a coating method according to theinvention according to method steps i) to iii) by applying a pressuredifference and a set pressure difference reversal (Pattern 1), has thelowest pressure loss, but is otherwise weaker in filtration efficiency,light-off temperature and OSC than the other Patterns 2 to 4. Thecombination of two layers with low permeability, which were eachproduced by applying a pressure difference via a coating method notaccording to the invention (Pattern 4), shows very good values withregard to light-off temperature, OSC and filtration efficiency, butresults in an enormous increase in pressure. The best combination of allfeatures (pressure loss, filtration efficiency, light-off temperatureand OSC) is shown surprisingly by the combination of a layer in theinput cell (inflow side of the filter in the exhaust gas) with lowpermeability, which was produced according to claim 6 by applying apressure difference with a layer in the output cell (outflow side of thefilter in the exhaust gas) with a high permeability/which was producedvia a coating method according to claim 1 method steps i) to iii). Theoptimum setting of the two zone lengths depends on the requirements ofthe respective motor. The quality criteria of the coated filter can thusbe adjusted via the zone length as with a shift regulator.

1. A method for producing a coated ceramic wall flow filter having atleast two catalytically active zones, the wall flow filter having afirst end face, a second end face and a length L and a porosity of atleast 50% to at most 80% and a mean pore diameter of 5 - 50 µm, themethod comprising the following steps in sequence: i) an excess of afirst coating suspension is introduced into the first end face byapplying a pressure difference via the wall flow filter; ii) with apressure difference reversal, an excess of the first coating suspensionis removed from the wall flow filter; iii) following a pause periodafter ii), a second coating suspension without excess is introduced intothe wall flow filter via the second end face by applying a pressuredifference via the wall flow filter.
 2. Method according to claim 1,wherein in step i), the first coating suspension is introduced into thevertically locked wall flow filter from the lower, first end face intothe wall flow filter, and in step iii) the second coating suspension isintroduced from the upper, second end face into the wall flow filter. 3.(canceled)
 4. Method according to claim 1, wherein the pressure pulsefor the pressure difference reversal is at least 150 mbar and at most400 mbar.
 5. Method according to claim 1, wherein a pressureless holdingtime before the pressure difference reversal of up to 10 seconds ismaintained.
 6. Method according to claim 1, wherein one zone has apositive gradient for the amount of catalytically active material in thecoating direction.
 7. Catalytically coated ceramic wall flow filter forthe treatment of exhaust gases of a combustion process producedaccording to claim
 1. 8. Catalytically active wall flow filter accordingto claim 7, wherein the catalytically active coatings of the filter areselected from the group consisting of three-way catalyst, SCR catalyst,nitrogen oxide storage catalyst, oxidation catalyst, soot-ignitioncoating, hydrocarbon storage.
 9. Catalytically active wall flow filteraccording to claim 8, wherein the catalytically active coatings arelocated in the pores and/or on the surfaces of the channel walls of thefilter.
 10. A method of oxidizing hydrocarbons and/or carbon monoxideand/or reducing nitrogen oxide by contacting an exhaust gas with thewall flow filter of claim
 7. 11. The method of claim 1, wherein thepause period includes drying the first coating suspension on the wallflow filter.
 12. The method of claim 11, wherein the pause periodincludes both drying and calcining the first coating suspension on thewall flow filter.
 13. The method of claim 1, wherein in step i) thefirst coating suspension travels up from the lower, first end face intothe wall flow filter, and each of steps ii) and iii) include a suctiondraw at the lower end of the wall flow filter.
 14. The method of claim13, wherein the suction draw level at step ii) is stronger than that atstep iii).
 15. The method of claim 14, wherein the suction pulse time atstep ii) is shorter in duration than that at step iii).
 16. The methodof claim 14, wherein the first coating suspension travels up from thelower, first end face into the wall flow filter due to an upwarddirected pressure application at the lower end face of the wall flowfilter.
 17. The method of claim 1, wherein the first coating suspensionhas a lesser solid content than the second coating suspension.
 18. Themethod of claim 1, wherein the first and second coating suspsensionshave different particle sizes such that one of the two coatingsuspension is an in-wall coating while the other is an on-wall coating.19. The method of claim 1, wherein the first coating suspension isapplied as to define a postivie gradiant that results in the firstcoating applied having less catallyticallly active material at the firstface end of the wall flow filter as compared to downstream relative to adirection of first coating suspension application.
 20. The method ofclaim 1, wherein the wall flow filter remains in a common orientationfor each of steps i), ii) and iii).
 21. The method of claim 1, whereinthe pause includes a drying, or drying and calcining, treatment afterii) and before the second coating is introduced in iii).
 22. The methodof claim 21, wherein, following step iii), the second coating suspensionis subjected to another drying, or drying and calcining, step.